SPLIT LINE SYSTEM, METHOD AND PROCESS FOR CO2 RECOVERY
A process, system or apparatus for recovering C02 from a gas has an absorption section, cooling section, regeneration section and more than three heating sections and involves a split in the C02 rich stream from the first heating section. A solvent for recovering C02 from a gaseous mixture comprising a primary amino hindered alcohol or tertiary amine in combination with a derivative of piperazine with three or more amino groups as promoter and a carbonate buffer is also disclosed.
1 . An apparatus for recovering C0 2 from a gas containing C0 2 , comprising:
(a) an absorption section comprising (i) an absorption tower having a top portion and a bottom portion (ii) a liquid feed where the gas contacts the liquid fed to form a C0 2 -rich solution,
(b) a cooling section where a C0 2 semi-rich solution is extracted downstream of the absorption section using a cooling medium and pumped back to the absorption section between the first point and the second point of the absorption tower,
(c) a regeneration section having a regenerator where the C0 2 rich solution is heated utilizing the heat from steam and to produce a C0 2 lean solution,
(d) a first heating section,
(e) a second heating section where a portion of C0 2 rich solution gets heated with the C02-lean solution coming from the regenerator,
(f) a third heating section where steam is supplied to heat the C02-rich solution traveling from the regenerator to further remove C02 and produce a leaner C02 solution and whereby steam condensate is produced from the steam due to loss of heat from the steam, and
(g) a fourth heating section where a portion of the C02-rich solution gets heated with the steam condensate from the third heating section.
2 . An apparatus according to claim 1 , wherein the apparatus is structured such that, after the first heating section, the C0 2 rich solution slits into (i) a first C0 2 rich solution (5-90% of mass flow) that is conveyed to a top section of the regenerator and a second C0 2 rich solution that is conveyed to the second heating section, (ii) the second C0 2 rich solution in a vapor-liquid phase by about 0-0.05 by volume is fed to the regenerator downstream of the first heating section.
3 . The apparatus according to claim 1 , wherein the C0 2 lean solution and the second C0 2 rich solution is conveyed to the second heating section.
4 . The apparatus according to claim 1 , further comprising a semi C0 2 lean solution conveying path drawn from downstream of the regenerator with 0-80% of the liquid flow and mixed with the second C0 2 -rich solution going to the second heating section.
3 . (canceled)
5 . The apparatus according to claim 1 , further comprising a semi C0 2 lean solution conveying path drawn from downstream of the regenerator with 0-80% of the liquid flow and mixing with the second C02-rich solution going to the second heating section at a point after the split.
6 . The apparatus according to claim 2 , wherein the heat steam condensate from the second heating section conveys the C02 solution into a first heating section and a second heating section.
7 . A C0 2 recovery process, comprising:
(a) Contacting a gas having C0 2 with a liquid solvent from an absorption tower, having a top section and an bottom section, to form a Co2-rich solution, wherein the absorption tower has an absorber,
(b) cooling the C0 2 -rich solution downstream of absorption tower using a cooling medium,
(c) leaning the C0 2 -rich solution by heating the C0 2 -rich solution in a regenerator using steam and releasing C0 2 upwards, from a third heating section,
(d) splitting the C0 2 -rich solution into a first C0 2 -rich solution conveyed to the first point on top section of the regenerator and a second portion of C02 rich solution,
(e) conveying the second C0 2 -rich solution to a second heating section wherein the second portion of C0 2 -rich solution gets heated with C0 2 lean solution coming from regenerator,
(f) heating the second C0 2 -rich solution in a second heating section, wherein the solutions has a vapor-liquid phase (0-0.05 by volume), and
(g) feeding the second C0 2 -rich solution to the regenerator at a second point downstream the splitting step (d).
8 . The process as claimed in claim 7 , pumping the Co2-rich solution to the absorber at a point between first and second points of the absorption tower.
9 . The process as claimed in claim 7 , further comprising supplying steam in a third heating section to heat the C02-rich solution from the regenerator in remove C02 and produce C02-lean solution, whereby a steam condensate is produced from the steam.
10 . The process as claimed in claim 7 , further comprising drawing the C02 lean solution from the bottom of regenerator and conveying the C02 lean solution to the second heating section.
11 . A solvent for recovery of carbon dioxide from gaseous mixture, comprising:
(a) Primary amino hindered alcohol
(b) Derivative of piperazine with three or more amino groups as promoter
(c) a carbonate buffer,
wherein the solvent contains less than about 75% by weight of water and has a single liquid phase.
12 . The solvent as claimed in claim 11 , wherein the primary amino hindered alcohol is 2-amino-2-methylpropanol (AMP), wherein the carbonate buffer is a potassium carbonate buffer and the promoter as defined in 8 is N aminoethylpiperazine (AEP),
13 . A solvent for recovery of carbon dioxide from gaseous mixture, comprising:
(a) Tertiary amine
(b) Derivative of piperazine with three or more amino groups as promoter
(c) A carbonate buffer,
wherein the solvent contains less than about 75% by weight of water and has a single liquid phase, the carbonate buffer is a potassium carbonate buffer, the tertiary amine compounds used in the present invention is N,N-diethyl ethanolamine (DEEA),
14 . The solvent as claimed in claim 13 , wherein the promoter as defined in claim 10 b is N-aminoethylpiperazine (AEP) and a carbonate buffer is potassium carbonate buffer.
15 . An system for recovering C0 2 from a gas containing C02, comprising:
(a) an absorption section comprising (i) an absorption tower having a top portion and a bottom portion (ii) a liquid feed where the gas comes in contact with the liquid absorbent fed from the first portion to form a C0 2 -rich solution,
(b) a cooling section where a C0 2 semi-rich solution is extracted downstream of the absorption section using a cooling medium and pumped back to the absorption section between the first point and the second point of the absorption tower,
(c) a regeneration section having a regenerator where the C0 2 rich solution is heated utilizing the heat from steam and to produce a C0 2 lean solution,
(d) a first heating section,
(e) a second heating section where a portion of C0 2 rich solution gets heated with C02-lean solution coming from regenerator,
(f) a third heating section where steam is supplied to heat the C0 2 -rich solution travelled from the regenerator to further remove C0 2 and produce a leaner C02solution and whereby steam condensate is produced from the steam due to loss of heat from the steam, and
(g) a fourth heating section where section portion of C0 2 -rich solution gets heated with the steam condensate from the third heating section.
16 . The apparatus according to claim 2 , wherein the apparatus is arranged to the heat steam condensate from the second heating section before splitting the C02 solution into the first and the second C02-rich solutions.